Thermoplastic polyurethanes

ABSTRACT

Thermoplastic polyurethanes are obtainable by reacting (a) isocyanates with (b1) polyesterdiols having a melting point greater than 150° C., (b2) polyetherdiols and/or polyesterdiols, each having a melting point of less than 150° C. and a molecular weight of from 501 to 8000 g/mol, and, if required, (c) diols having a molecular weight of from 62 to 500 g/mol.

BACKGROUND OF THE INVENTION

(1) Field of the Invention

The present invention relates to thermoplastic polyurethanes obtainable by reacting (a) isocyanates with (b1) polyesterdiols having a melting point greater than 150° C., preferably from 151 to 260° C., particularly preferably from 165 to 245° C., (b2) polyetherdiols and/or polyesterdiols, each having a melting point of less than 150° C., preferably from 0 to 149° C., and a molecular weight of from 501 to 8000 g/mol, and, if required, (c) diols having a molecular weight of from 62 to 500 g/mol. The present invention furthermore relates to a process for the preparation of thermoplastic polyurethanes and products containing the novel thermoplastic polyurethanes.

(2) Description of Related Art

Thermoplastic elastomers are based on a standard structural principle, regardless of their chemical composition. They are block copolymers in which hard blocks are connected to soft blocks in a polymer chain. Hard blocks are to be understood as meaning polymer segments whose softening temperature—glass transition temperature or crystallite melting point—is far above the temperature of use. Soft blocks are polymer segments having softening temperatures well below the temperature of use, preferably less than 0° C. The hard blocks form physical networks which can be reversibly cleaved during the thermoplastic processing and reformed on cooling.

Typical examples are styrene/butadiene block copolymers having hard polystyrene blocks (glass transition temperature about 105° C.) and soft polybutadiene blocks (glass transition temperature about −90° C.) or thermoplastic polyurethanes (TPU). The latter product group has, as a semicrystalline hard phase, the reaction product of an organic diisocyanate with a low molecular weight diol and, as an amorphous soft phase, the reaction product of an organic diisocyanate with a polyesterdiol or a polyetherdiol having molecular weights of, usually, from 500 to 5000 g/mol.

The solidification behavior of this semicrystalline polyurethane hard phase is however very variable and can easily be influenced, deteriorations generally occurring. For example, an increase in the index (ratio of moles of isocyanate to moles of OH-containing components) to the range of from 1.05 to 1.20 has a very adverse effect, as does the addition of other polymers. The conventional preparation processes, such as belt and extruder processes, also lead, with the same formulation, to TPU having substantially different crystallization behavior. However, in all processing methods, whether injection molding or extrusion, a constant and rapid solidification rate is a substantial factor influencing the uniform quality of the shaped articles, properties such as hardness, strength, rigidity and heat distortion resistance, and the cost-efficiency of the production.

A wide range of efforts has been made to compensate this disadvantageous behavior of the TPU. Apart from the addition of nucleating agents, e.g. finely divided talc, attempts have also been made to achieve improvements by adding other, rapidly crystallizing polymers. Thermoplastic, semicrystalline polyesters were particularly frequently used, among these preferably polybutylene terepthalate, owing to its melting range of from 220 to 230° C. which very well matches the customary TPU processing temperatures.

Thus, DE-A 26 46 647 describes the compounding of prepared, high molecular weight polyesters and high molecular weight TPU in single-screw or twin-screw extruders. EP-A 334 186 and DE-A 41 13 891 disclose the compounding of high molecular weight polyesters and TPU monomer components. DE-A 41 28 274 describes the addition of up to 5% of diisocyanate in excess for such processes. For an improvement in the compatibility, EP-A 656 397 describes the use of a TPU having an index greater than 1.16 and admixture with high molecular weight polyester. These processes lead to two-phase polymer mixtures, the polymer component, when present in amounts greater than 50%, having particle sizes of from 10 to 50 μm or <5 μm with the use of additional diisocyanate. Such molding materials are said to have higher strength, rigidity and heat distortion resistance than an unmodified TPU. On the other hand, the fact that a substantial reduction in the solidification rate occurs in particular on addition of diisocyanate in excess is very disadvantageous.

EP-A 102 115 and EP-A 846 712 describe the reaction of polyalkylene terephthalates with aliphatic polyesters to give block copolyester-esters, which in turn are then reacted with organic diisocyanates. The polycondensation of dimethyl terephthalate, butanediol and polyetherdiol and the subsequent reaction of the polyester with further polyetherdiol and diisocyanates to give a high molecular weight product are described in WO 99/51656. The long reaction times and the high temperatures, which easily lead to pronounced discoloration of the molding materials, are disadvantageous in all these processes.

DE-A 199 39 112 describes the degradation of hard thermoplastic polyurethanes with low molecular weight diols and the subsequent reaction with isocyanates for the preparation of flexible TPU.

BRIEF SUMMARY OF THE INVENTION

It is an object of the present invention to provide thermoplastic polyurethanes having improved crystallization behavior of the hard phase and a very constant and rapid solidification rate during processing.

DETAILED DESCRIPTION OF THE INVENTION

We have found that this object is achieved by the thermoplastic polyurethanes described at the outset.

Thermoplastic polyurethanes in which the molar ratio of the diols (c) having a molecular weight of from 62 to 500 g/mol to the component (b2) is less than 0.2, particularly preferably from 0.1 to 0.01, are preferred.

Thermoplastic polyurethanes in which the polyesterdiols (b1), which preferably have a molecular weight of from 1000 to 5000 g/mol, have the following structural unit (I):

where

-   R₁ is a carbon skeleton of 2 to 15 carbon atoms, preferably an     alkylene group of 2 to 15 carbon atoms and/or a bivalent aromatic     radical of 6 to 15, particularly preferably 6 to 12, carbon atoms, -   R₂ is a straight-chain or branched alkylene group of 2 to 8,     preferably 2 to 6, particularly preferably 2 to 4, carbon atoms, in     particular —CH₂—CH₂— and/or —CH₂—CH₂—CH₂—CH₂—, -   R₃ is a straight-chain or branched alkylene group of 2 to 8,     preferably 2 to 6, particularly preferably 2 to 4, carbon atoms, in     particular —CH₂—CH₂— and/or —CH₂—CH₂—CH₂—CH₂—, and -   X is an integer from 5 to 30. In this preferred embodiment, the     melting point described at the outset and according to the invention     and/or the molecular weight according to the invention relate to the     structural unit (I) shown.

In this document, the term melting point is to be understood as meaning the maximum of the melting peak of a heating curve which was measured using a commercial apparatus (e.g. DSC 7/Perkin-Elmer), preferably a DSC apparatus, and evaluated according to ISO 11357-3.

The molecular weights stated in this document are the number average molecular weights in [g/mol].

The novel thermoplastic polyurethanes can preferably be prepared by

-   (i) reacting a preferably high molecular weight, preferably     semicrystalline, thermoplastic polyester with a diol (c) and then -   (ii) reacting the reaction product from (i) containing (b1)     polyesterdiol having a melting point greater than 150° C. and, if     required, (c) diol together with (b2) polyetherdiols and/or     polyesterdiols, each having a melting point of less than 150° C. and     a molecular weight of from 501 to 80000 g/mol, and, if required,     further (c) diols having a molecular weight of from 62 to 500 g/mol     with (a) isocyanate, in the presence or absence of (d) catalysts     and/or (e) assistants.

In the reaction (ii), the molar ratio of the diols (c) having a molecular weight of from 62 to 500 g/mol to the component (b2) is preferably less than 0.2, especially from 0.1 to 0.01.

Whereas the hard phases are provided for the end product by the step (i), by the polyester used in step (i), the soft phases are synthesized by the use of the component (b2) in step (ii). In the novel technical procedure, polyesters having a pronounced, readily crystallizing hard phase structure are melted, preferably in a reaction extruder, and are first degraded with a low molecular weight diol to give shorter polyesters having free terminal hydroxyl groups. Here, the original high tendency of the polyester to crystallize is retained and can subsequently be utilized for obtaining, in a rapid reaction, TPU having the advantageous properties, such as high tensile strength values, low abrasion values and, owing to the high and narrow melting range, high heat distortion resistances and low compression sets. Thus, in the novel process, high molecular weight, semicrystalline, thermoplastic polyesters are preferably degraded with low molecular weight diols (c) under suitable conditions in a short reaction time to give rapidly crystallizing polyester diols (b1), which in turn are then incorporated, with other polyesterdiols and/or polyetherdiols and diisocyanates, into high molecular weight polymer chains.

The thermoplastic polyester used preferably has, i.e. before the reaction of (i) with the diol (c), a molecular weight of from 15000 to 40000 g/mol and preferably a melting point greater than 160° C., particularly preferably from 170 to 260° C.

Generally known, preferably high molecular weight, preferably semicrystalline, thermoplastic polyesters, for example in granulated form, can be used as starting material, i.e. as polyester which is reacted in step (i), preferably in the molten state, particularly preferably at from 230 to 280° C., preferably for from 0.1 to 4 minutes, particularly preferably from 0.3 to 1 minute, with the diol or diols (c). Suitable polyesters are based, for example, on aliphatic ω-hydroxycarboxylic acids and/or on aliphatic, cycloaliphatic, araliphatic and/or aromatic dicarboxylic acids, for example lactic acid and/or terephthalic acid, and aliphatic, cycloaliphatic, araliphatic and/or aromatic dialcohols, for example 1,2-ethanediol, 1,4-butanediol and/or 1,6-hexanediol.

Particularly preferably used polyesters are poly-L-lactic acid and/or polyalkylene terephthalate, for example polyethylene terephthalate, polypropylene terephthalate or polybutylene terephthalate, in particular polybutylene terephthalate.

The preparation of these esters from said starting materials is generally known to a person skilled in the art and is widely described. Suitable polyesters are furthermore commercially available.

The thermoplastic polyester is melted, preferably at from 180 to 270° C. The reaction (i) with the diol (c) is preferably carried out at from 230 to 280° C., preferably from 240 to 280° C.

Generally known diols having a molecular weight of from 62 to 500 g/mol, for example those mentioned below, e.g. ethylene glycol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol, 1,6-hexanediol, heptanediol, octanediol, preferably 1,4-butanediol and/or 1,2-ethanediol, may be used as diol (c) in step (i) for the reaction with the thermoplastic polyester and, if required, in step (ii).

The weight ratio of the thermoplastic polyester to the diol (c) in step (i) is usually from 100:1.0 to 100:10, preferably from 100:1.5 to 100:8.0.

The reaction of the thermoplastic polyester with the diol (c) in the reaction step (i) is preferably carried out in the presence of conventional catalysts, for example those which are described below. Catalysts based on metals are preferably used for this reaction. The reaction in step (i) is preferably carried out in the presence of from 0.1 to 2% by weight, based on the weight of the diol (c), of catalysts. The reaction in the presence of such catalysts is advantageous for enabling the reaction to be carried out in the available short residence time in the reactor, for example a reaction extruder.

Examples of suitable catalysts for this reaction step (i) are tetrabutyl orthotitanate and/or tin(II) dioctanoate, preferably tin dioctanoate.

The polyesterdiol (b1) as a reaction product from (i) preferably has a molecular weight of from 1000 to 5000 g/mol. The melting point of the polyesterdiol as a reaction product from (i) is preferably from 150 to 260° C., particularly preferably from 151 to 260° C., in particular from 165 to 245° C., i.e. the reaction product of the thermoplastic polyester with the diol (c) in step (i) contains compounds having said melting point which are used in the subsequent step (ii).

As a result of the reaction of the thermoplastic polyester with the diol (c) in step (i), the polymer chain of the polyester is cleaved by transesterification by the diol (c). The reaction product of the TPU therefore has free terminal hydroxyl groups and is further processed according to the invention in the further step (ii) to give the actual product, the TPU.

The reaction of the reaction product from step (i) in step (ii) is effected, according to the invention, by adding (a) isocyanate (a) and (b2) polyetherdiols and/or polyesterdiols, each having a melting point of less than 150° C. and a molecular weight of from 501 to 8000 g/mol, and, if required, further diols (c) having a molecular weight of from 62 to 500, (d) catalysts and/or (e) assistants to the reaction product from (i). The reaction of the reaction product with the isocyanate is effected via the terminal hydroxyl groups formed in step (i). The reaction in step (ii) is preferably effected at from 190 to 250° C., preferably for from 0.5 to 5, particularly preferably from 0.5 to 2, minutes, preferably in a reaction extruder, particularly preferably in the same reaction extruder in which the step (i) was also carried out. For example, the reaction of step (i) can be effected in the first barrels of a conventional reaction extruder and the corresponding reaction of step (ii) can be carried out at a downstream point, i.e. in downstream barrels, after the addition of the components (a) and (b2). For example, the first 30 to 50% of the length of the reaction extruder can be used for step (i) and the remaining 50 to 70% can be employed for step (ii).

The reaction in step (ii) is preferably effected with an excess of the isocyanate groups relative to the groups reactive toward isocyanates. In the reaction (ii), the ratio of the isocyanate groups to the to the hydroxyl groups is from 1:1 to 1.2:1, particularly preferably from 1.02:1 to 1.2.1.

The reactions (i) and (ii) are preferably carried out in a generally known reaction extruder. Such reaction extruders are described by way of example in Werner & Pfleiderer's company publications or in DE-A 2 302 564.

The novel process is preferably carried out in such a way that at least one thermoplastic polyester, e.g. polybutylene terephthalate, is metered into the first barrel of a reaction extruder and is melted at, preferably, from 180 to 270° C., especially from 240 to 270° C., a diol (c), e.g. butanediol, and preferably a transesterification catalyst are added to a downstream barrel, the polyester is degraded by the diol (c) at from 240 to 280° C. to give polyester oligomers having terminal hydroxyl groups and molecular weights of from 1000 to 5000 g/mol, isocyanate (a) and (b2) compounds reactive toward isocyanates and having a molecular weight of from 501 to 8000 g/mol and, if required, (c) diols having a molecular weight of from 62 to 500, (d) catalysts and/or (e) assistants are metered into a downstream barrel and the synthesis to give the novel thermoplastic polyurethanes is then carried out at from 190 to 250° C.

In step (ii), no (c) diols having a molecular weight of from 62 to 500 are fed in, with the exception of the (c) diols having a molecular weight of from 62 to 500 which are contained in the reaction product of (i).

The reaction extruder preferably has neutral and/or backward-conveying kneading blocks and backward-conveying elements in the region in which the thermoplastic polyester is melted and preferably screw mixing elements, toothed disks and/or toothed mixing elements in combination with backward-conveying elements in the region in which the thermoplastic polyester is reacted with the diol.

Downstream of the reaction extruder, the clear melt is usually fed by means of a gear pump to an underwater granulation stage and is granulated.

The novel thermoplastic polyurethanes have optically clear, single-phase melts which rapidly solidify and, owing to the semicrystalline hard polyester phase, form slightly opaque to white opaque moldings. The rapid solidification behavior is a decisive advantage compared with known formulations and preparation processes for thermoplastic polyurethanes. The rapid solidification behavior is so pronounced that even products having hardnesses of from 50 to 60 Shore A can be processed by injection molding with cycle times of less than 35 seconds. In extrusion too, for example in the production of blown films, no TPU-typical problems such as adhesion or blocking of the films or tubes occur.

The amount of the thermoplastic polyester in the end product, i.e. the thermoplastic polyurethane, is preferably from 5 to 75% by weight. The novel thermoplastic polyurethanes are particularly preferably products of the reaction of a mixture containing from 10 to 70% by weight of the reaction product from (i), from 10 to 80% by weight of (b2) and from 10 to 20% by weight of (a), the stated weights being based on the total weight of the mixture containing (a), (b2), (d), (e) and the reaction product from (i).

The novel thermoplastic polyurethanes preferably have a hardness of from Shore 45 A to Shore 78 D, particularly preferably from 50 A to 75 D.

The novel thermoplastic polyurethanes preferably have the following structural unit (II):

where

-   R₁ is a carbon skeleton of 2 to 15 carbon atoms, preferably an     alkylene group of 2 to 15 carbon atoms and/or an aromatic radical of     6 to 15 carbon atoms, -   R₂ is a straight-chain or branched alkylene group of 2 to 8,     preferably 2 to 6, particularly preferably 2 to 4, carbon atoms, in     particular —CH₂—CH₂— and/or —CH₂—CH₂—CH₂—CH₂—, -   R₃ is a straight-chain or branched alkylene group of 2 to 8,     preferably 2 to 6, particularly preferably 2 to 4, carbon atoms, in     particular —CH₂—CH₂— and/or —CH₂—CH₂—CH₂—CH₂—, -   R₄ is a radical which arises from the use of polyetherdiols and/or     polyesterdiols, each having molecular weights of from 501 to 8000     g/mol, as (b2), or from the use of alkanediols of 2 to 12 carbon     atoms, -   R₅ is a carbon skeleton of 2 to 15 carbon atoms, preferably an     alkylene group of 2 to 15 carbon atoms and/or a bivalent aromatic     radical of 6 to 18, particularly preferably 6 to 15, carbon atoms, -   X is an integer from 5 to 30 and -   n and m are each an integer from 5 to 20.

R₁, R₂ and R₃ are defined by the reaction product of the thermoplastic polyester with the diol (c) in (i), R₄ is defined by the starting components (b2) and, if required, (c) and R₅ is defined by the isocyanate used.

The novel product of step (ii), i.e. the TPU, can be extruded, cooled and granulated.

The processing of TPU prepared according to the invention to give the desired films, fibers, shaped articles, claddings in automobiles, rollers, seals, cable plugs, bellows, tubes, cable sheaths, trailing cables, belts or damping elements, in particular films, can be effected by conventional methods, for example injection molding, extrusion, spinning process or sinter process, which is also known as a powder slush process.

The components (a), (b2), (c), (d) and/or (e) usually used in the preparation of the TPU are to be described below by way of example:

-   a) Organic isocyanates (a) used are conventional aliphatic,     cycloaliphatic, araliphatic and/or aromatic isocyanates, preferably     diisocyanates, for example tri-, tetra-, penta-,     2-methylpentamethylene 1,5-diisocyanate, 2-ethylbutylene     1,4-diisocyanate, pentamethylene 1,5-diisocyanate, butylene     1,4-diisocyanate,     1-isocyanato-3,3,5-trimethyl-5-isocyanatomethylcyclohexane     (isophorone diisocyanate, IPDI), 1,4- and/or     1,3-bis(isocyanatomethyl)cyclohexane (HXDI), cyclohexane     1,4-diisocyanate, 1-methylcyclohexane 2,4- and/or 2,6-diisocyanate,     dicyclohexylmethane 4,4′-, 2,4′- and/or 2,2′-diisocyanate,     diphenylmethane 2,2′-, 2,4′- and/or 4,4′-diisocyanate (MDI),     naphthylene 1,5-diisocyanate (NDI), tolylene 2,4- and/or     2,6-diisocyanate (TDI), diphenylmethane diisocyanate,     dimethylbiphenyl 3,3′-diisocyanate, diphenylethane 1,2-diisocyanate     and/or phenylene diisocyanate, preferably diphenylmethane 2,2′-,     2,4′- and/or 4,4′-diisocyanate (MDI) and/or hexamethylene     diisocyanate (HDI). -   b) Those compounds (b2) reactive toward isocyanates which are used     in addition to the novel polyesterdiols (b1) are, for example,     polyhydroxy compounds, also referred to as polyols, having molecular     weights of from 501 to 8 000, preferably from 700 to 6000, in     particular from 800 to 4000, and preferably an average functionality     of from 1.8 to 2.6, preferably from 1.9 to 2.2, in particular 2. The     term functionality is to be understood in particular as meaning the     number of active hydrogen atoms, in particular hydroxyl groups.     Polyesterols and/or polyetherols and/or polycarbonatediols are     preferably used as (b2), particularly preferably polyesterdiols, for     example polycaprolactone, and/or polyetherpolyols, preferably     polyetherdiols, for example those based on ethylene oxide, propylene     oxide and/or butylene oxide, preferably polypropylene glycol, in     particular polyetherols. Compounds to are suitable for synthesizing     a soft phase in the TPU are particularly preferably used as (b2),     for example copolyesters based on adipic acid and mixtures of     1,2-ethanediol and 1,4-butanediol, copolyesters based on adipic acid     and mixtures of 1,4-butanediol and 1,6-hexanediol, polyesters based     on adipic acid and 3-methyl-1,5-pentanediol and/or     polytetramethylene glycol (polytetrahydrofuran, PTHF), particularly     preferably copolyesters based on adipic acid and mixtures of     1,2-ethanediol and 1,4-butanediol and/or polytetramethylene glycol     (PTHF). -   c) Compounds generally known as chain extenders, for example     alkanediols of 2 to 12, preferably 2, 3, 4 or 6, carbon atoms, can     be used as diols (c), it also being possible to use mixtures of said     compounds. Examples are the following compounds: ethane-1,2-diol,     propane-1,3-diol, hexane-1,6-diol and butane-1,4-diol. -   d) Suitable catalysts which in particular accelerate the reaction     between the NCO groups of the diisocyanates (a) and the hydroxyl     groups of the components (b2) and (b1) are the conventional tertiary     amines known from the prior art, e.g. triethylamine,     dimethylcyclohexylamine, N-methylmorpholine,     N,N′-dimethylpiperazine, 2-(dimethylaminoethoxy)ethanol,     diazabicyclo[2.2.2]octane and the like, and in particular organic     metal compounds, such as titanic acid esters. Apart from the     reaction in step (i), the catalysts are usually used in amounts of     from 0.0001 to 5 parts by weight per 100 parts by weight of     polyhydroxy compound (b).     -   Suitable catalysts which accelerate the degradation reaction of         the preferably high molecular weight, preferably         semicrystalline, thermoplastic polyesters with the component (c)         are in particular organic metal compounds, such as titanic acid         esters, e.g. tetrabutyl orthotitanate, iron compounds, e.g.         iron(III) acetylacetonate, tin compounds, e.g. tin diacetate,         tin dioctanoate, tin dilaurate or the dialkyltin salts of         aliphatic carboxylic acids, such as dibutyltin diacetate,         dibutyltin dilaurate or the like. -   e) In addition to catalysts, conventional assistants (e) may also be     added to the components (a) and (b2). Examples are surface-active     substances, flameproofing agents, antistatic agents, nucleating     agents, lubricants and mold release agents, dyes and pigments,     inhibitors, hydrolysis stabilizers, light stabilizers, heat     stabilizers, antioxidants or stabilizers for preventing     discoloration, agents for protecting from microbial degradation,     inorganic and/or organic fillers, reinforcing materials and     plasticizers.

Further information concerning the abovementioned assistants is to be found in the technical literature.

Mixtures containing the novel thermoplastic polyurethanes and at least one further thermoplastic material, for example polyolefins, polyester, polyamide, polyoxymethylene, polystyrene and/or styrene copolymers, are furthermore according to the invention.

The advantages according to the invention are to be described with reference to the examples below.

EXAMPLES

The preparation of examples 1 to 21 described below was carried out in a twin-screw extruder of type ZSK 58 from Werner & Pfleiderer. The length of the extruder process part was 12 barrels and the length of the barrels themselves was 4 times the screw diameter. The screw discharge from the extruder was carried out by means of a gear pump; the granulation was effected in a conventional underwater granulation means. The resulting granules were then dried in a fluidized-bed dryer at from 60 to 100° C. and in residence times of from 5 to 10 minutes to water contents of <0.03% and then heated for 15 hours at 80° C.

The temperatures of extruder barrel 1 was 260° C., that of barrels 2–4 was 250° C., that of barrel 5 was 240° C., that of barrels 6–12, including the melt discharge means, was 230° C. Under these conditions, the melt temperature of 220–230° C. resulted in the case of a throughput of about 200 kg/h and a speed of 200 rpm.

The semicrystalline, high molecular weight polyester used was a commercial polybutylene terephthalate (Ultradur® B 4500/BASF Aktiengesellschaft), the low molecular weight diol used for degrading the high molecular weight PBT was 1,4-butanediol and the aromatic diisocyanate used was 4,4′-diisocyanatodiphenyl-methane (MDI). The polydiols (PDO) used are described and characterized in table 1.

TABLE 1 Number av. mol. weight OH number Designation Composition M_(n) (g/mol) (mg KOH/1 g) PD0 1 Polyester of adipic acid, 2000 56.1 ethylene glycol and 1,4-butanediol (molar ratio 1:1) PD0 2 Polyester of adipic acid, 2000 56.1 1,4-butanediol and 1,6-hexanediol (molar ratio 2:1) PD0 3 Polyester of adipic acid and 2000 56.1 3-methyl-1,5-pentanediol PD0 4 Polyetherdiol based on 1000 112.2 polytetramethylene glycol

In example 1, the degradation of the Ultradure® B 4500 by 1,4-butanediol is described and the degradation products are characterized.

Ultradur® granules were metered continuously into the barrel 1 of the twin-screw extruder, 1,4-butanediol together with tin dioctanoate as a catalyst for accelerating the degradation was metered into barrel 3 and melt samples were taken from the opened barrel 5. The residence time of the melt (barrels 1–5) was about 44 seconds.

TABLE 2 Tin ULTRADUR ® B 4500 1,4-Butanediol dioctanoate Sample No. kg/h kg/h g/h 1 40 0 0 2 40 1.20 4.0 3 40 1.80 4.0 4 40 2.40 4.0

For the determination of unconverted 1,4-butanediol, in each case 10 g of melt sample were powdered and then suspended in 30 g of isopropanol and stirred for 48 hours at room temperature for complete extraction of the butanediol. In the isopropanol solution, butanediol was determined by gas chromatography. The insoluble fraction was filtered off, washed with isopropanol and completely dried for several hours at 100° C. The following determinations were carried out on these extracted samples:

-   Viscosity number VN:     -   A solution viscosity (ml/g) of 0.5% strength solution in         phenol/chlorobenzene (1:1) at 25° C., measured using an         Ubbelohde viscometer -   Terminal group analysis:     -   Dissolution in dichlorobenzene at 190° C., reaction with acetic         anhydride and titration with 0.1 nNaOH solution -   GPC analysis:     -   Eluent hexafluoroisopropanol +0.5% of potassium         trifluoroacetate, calibration with PMMA standards having a         narrow molecular weight distribution

TABLE 3 Content of Viscosity Terminal groups Mn values Sam- unconverted number Acid from ple butanediol VN Hydroxyl mmol/ terminal from No. (% by wt.) (ml/g) mmol/kg kg groups GPC 1 — 101 60.6 32.1 21600 16800 2 0.29 26.7 485 16.0 4000 3700 3 0.75 19.6 675 17.8 2900 2700 4 0.85 16.0 848 21.4 2300 2200

The values in table 3 show that, in the novel process, the high molecular weight polybutylene terephthalate can be degraded within the short residence time to give polyester chains having substantially terminal hydroxyl groups and Mn values of from 2000 to 4000.

Examples 2 to 4 below describe how samples no. 2, 3 and 4 are further reacted according to the invention by adding polyesterdiol, MDI and tin dioctanoate in barrel 5 of the twin-screw extruder.

TABLE 4 Ultradur ® Tin dioctanoate Polyesterdiol B 4500 Butanediol Barrel 3 Barrel 5 PD02 MDI Molar ratio Example No. kg/h kg/h g/h g/h kg/h kg/h MDI/(BD0 + PD02) 2 40 1.20 4.0 4.0 128.7 20.80 1.07 3 40 1.80 4.0 4.0 128.7 22.58 1.07 4 40 2.40 14.0 4.0 128.7 24.36 1.07 5 40 — — 4.0 128.7 17.23 1.07 BD0 = Butanediol

In example 5 not according to the invention, Ultradur B 4500 was reacted with PDO 2 and MDI without degradation by butanediol but under otherwise identical reaction conditions. In contrast to the visually clear and single-phase melts from examples 2 to 4, the melt according to example 5 was opaque white, nontransparent and two-phase. After a run time of only a few minutes, agglomeration of the extremely tacky granular particles occurred in the underwater granulation means and the experiment had to be terminated. The product obtained up to then could not be processed by injection molding. For comparative measurements, 2 mm thick test plates were produced by pressing at about 190–200° C.

For the determination of the mechanical properties, the experimental products were processed in a conventional manner by injection molding to give test specimens, which were heated for 20 hours at 100° C. before the test.

The tests were carried out under the following conditions:

-   Hardness:     -   Shore A or Shore D, measured according to DIN 53505 -   TS:     -   Tensile strength (MPa), measured according to DIN 53504 -   EB:     -   Elongation at break (%), measured according to DIN 53504 -   TPS:     -   Tear propagation strength (N/mm), measured according to DIN         53515 -   Abrasion:     -   Abrasion (mm³), measured according to DIN 53516 -   DSC     -   Measured using a DSC 7 apparatus from -   values:     -   Perkin-Elmer and evaluated according to ISO 11357-3;     -   Heating and cooling rates: 20° K/min.     -   T_(M): Melting peak maximum (° C.) from the 2nd heating curve     -   T_(Kmax): Crystallization peak maximum (° C.) from the cooling         curve

These conditions apply to examples 2 to 5 as well as to all examples below.

TABLE 5 Example Hard- DSC values No ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 2 67 A 19 850 41 57 329 209 165 3 71 A 23 880 50 47 328 196 134 4 73 A 25 840 51 47 337 186 119 5 58 A 8 800 10 >500 222 212 159

The values of the novel experimental products (examples 2–4) exhibit an excellent property level, in particular with regard to the solidification behavior in injection molding.

The values of example 5 not according to the invention show that it is merely a physical mixture of a high molecular weight PBT with a high molecular weight polyurethane soft phase, resulting not only in the extreme tack but also in the low tensile strength, low tear propagation strength and extremely high abrasion.

In examples 6 to 9 below, it is intended to show that products having a hardness of from Shore 44 D to 75 D can be prepared by the novel process.

TABLE 6 Ultradur ® Tin dioctanoate Polyesterdiol B 4500 Butanediol Barrel 3 Barrel 5 PD02 MDI Molar ratio Example No. kg/h kg/h g/h g/h kg/h kg/h MDI/(BD0 + PD02) 6 65.7 3.30 4.0 4.0 56.0 17.1 1.06 7 75.0 4.50 4.0 4.0 43.7 19.0 1.06 8 87.0 5.22 4.0 4.0 30.60 19.43 1.06 9 99.0 5.94 4.0 4.0 19.40 20.06 1.06

In addition to the substances stated in table 6, 1.45 kg/h of a powder mixture consisting of 25% of a finely divided talc (talc IT extra from Omya), 25% of an antioxidant (Irganox® 1010 from Ciba-Geigy) and 50% of a lubricant and mold release agent (Uniwax 1760 from Uniqema) were added to barrel 8 of the twin-screw extruder via a laterally mounted screw metering apparatus. The total throughput was then 144–146 kg/h.

TABLE 7 Example Hard- DSC values No. ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 6 44 D 32 590 112 15 271 190 140 7 54 D 38 410 151 18 249 189 142 8 66 D 49 440 183 16 241 193 150 9 75 D 45 430 251 20 229 195 155

In example 10 to 17 below, it is intended to show that products having a hardness of from Shore 50 A to 80 A can be prepared by the novel process.

TABLE 8 Ultradur ® Tin dioctanoate Polyesterdiol B 4500 Butanediol Barrel 3 Barrel 5 PD01 MDI Molar ratio Example No. kg/h kg/h g/h g/h kg/h kg/h MDI/(BD0 + PD01) 10 20.0 1.20 4.0 4.0 146.9 24.24 1.116 11 27.0 1.62 4.0 4.0 139.3 24.48 1.116 12 33.0 1.98 4.0 4.0 132.7 24.66 1.116 13 40.0 2.40 4.0 4.0 125.0 24.90 1.116

TABLE 9 Ultradur ® Tin dioctanoate Polyesterdiol Polyesterdiol Example B 4500 Butanediol Barrel 3 Barrel 5 PD0 2 PD0 3 MDI Molar ratio MDI No. kg/h kg/h g/h G/h kg/h kg/h kg/h (BD0 + PD02 + PD03) 14 22.0 1.10 4.0 4.0 118.2 29.5 23.05 1.07 15 27.5 1.38 4.0 4.0 114.1 28.5 23.20 1.07 16 33.0 1.65 4.0 4.0 109.2 27.3 23.18 1.07 17 36.5 1.86 4.0 4.0 106.4 26.6 23.33 1.07 In addition to the substances stated in tables 8 and 9, 2.00 kg/h of a powder mixture which has been described above in the case of examples 6 to 9 were introduced into barrel 8 of the twin-screw extruder.

TABLE 10 Example Hard- DSC values No. ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 10 57 A 23 880 41 36 461 200 155 11 65 A 25 820 46 35 476 195 140 12 71 A 23 850 53 33 472 200 150 13 77 A 31 860 62 35 458 197 144 14 52 A 19 1240 24 104 387 195 139 15 56 A 18 1330 31 82 354 198 145 16 65 A 26 1060 37 68 361 201 153 17 69 A 28 1080 41 68 348 197 155 In addition to good mechanical properties, the products according to examples 10 to 17 show pronounced and very good solidification and crystallization behavior which has a very positive effect on the processing behavior in injection molding and in extrusion, as will be shown below. Examples 14 to 17 demonstrate that mixtures of polyesterdiols having different chemical structures can also be used in the novel process. This is sometimes important for suppressing subsequent crystallization of the originally amorphous polyurethane soft phase and hence subsequent hardening during storage of the products.

In addition to polyesterdiols, polyetherdiols or polyesterdiol/polyetherdiol mixtures can also be used in the novel process, as will be explained with reference to examples 18 to 20.

TABLE 11 Ultradur ® Tin dioctanoate Polyesterdiol B 4500 Butanediol Barrel 3 Barrel 5 PD04 MDI Molar ratio Example No. kg/h kg/h g/h g/h kg/h kg/h MDI/(BD0 + PD04) 18 34.0 2.76 4.0 4.0 118.2 39.48 1.06 19 50.0 4.02 4.0 4.0 101.6 38.79 1.06 20 70.0 5.64 4.0 4.0 80.74 38.02 1.06 In addition to the substances stated in table 11, 2.00 kg/h of a powder mixture as described in the case of examples 6 to 9 were introduced into barrel 8 of the twin-screw extruder.

TABLE 12 Example Hard- DSC value No. ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 18 70 A 40 710 38 30 1603 178 71 19 80 A 43 610 64 27 1282 176 75 20 90 A 50 470 74 30 640 180 80

In example 21 below, it is intended to show that a commercial polyethylene terephthalate (polyester type RT 51 from Kosa) can be reacted according to the novel process.

TABLE 13 PET Tin dioctanoate Polyesterdiol Polyesterdiol Example RT 51 Butanediol Barrel 3 Barrel 5 PD0 2 PD0 3 MDI Molar ratio MDI/ No. kg/h kg/h g/h g/h kg/h kg/h kg/h (BD0 + PD0 2 + PD0 3) 21 36.5 2.92 12.0 4.0 105.4 26.3 25.33 1.03

Owing to the higher melting range of polyethylene terephthalate, the temperature profile of the twin-screw extruder was changed in the following manner:

Barrels 1 to 4: 270° C. Barrel 5: 260° C. Barrels 6 to 12: 250° C. Melt discharge means: 230° C.

In addition to the substances stated in table 13, 2.00 kg/h of a powder mixture as described in the case of examples 6 to 9 were introduced into barrel 8 of the twin-screw extruder.

TABLE 14 Example Hard- DSC values No ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 21 68 A 15 960 24 120 230 238 196

In examples 22 to 24 below, it is intended to show that an aliphatic diisocyanate/hexamethylene 1,6-diisocyanate (HDI) can be reacted according to the novel process.

TABLE 15 Ultradur ® Tin dioctanoate Polyesterdiol B 4500 Butanediol Barrel 3 Barrel 5 PD02 HDI Molar ratio Example No. kg/h kg/h g/h g/h kg/h kg/h HDI/(BD0 + PD02) 22 37.5 2.25 4.0 12.0 95.8 12.38 1.01 23 45.0 2.70 4.0 12.0 87.7 12.53 1.01 24 52.5 3.15 4.0 12.0 79.5 12.69 1.01

TABLE 16 Example Hard- DSC values No ness TS EB TPS Abrasion VN T_(M) T_(Kmax) 22 79 A 13 950 41 100 150 179 71 23 84 A 15 880 50 52 163 179 68 24 89 A 19 820 60 41 148 182 63

The present examples 2 to 24 show that block copolymers which differ from the commercial thermoplastic polyurethanes in that the customary hard phase segment, consisting of butanediol/MDI units, was exchanged for semicrystalline, rapidly crystallizing, hard polyester segments can be prepared by the novel process.

It is possible to prepare products which cover a hardness range of from Shore 50 A to Shore 75 D and have elastomeric behavior, in particular the advantageous properties of the commercial thermoplastic polyurethanes, such as high strengths in combination with high elongation at break, high tear propagation strengths and high abrasion resistances.

However, the advantage over the commercial thermoplastic polyurethanes is based on the narrow melting range and the tendency of the semicrystalline polyester hard phase to crystallize, so that problem-free and rapid processing by injection molding and by extrusion is possible even in the case of very soft products having a hardness of from Shore 50 A to Shore 75 A.

These advantageous processing properties are to be explained in examples 25 and 26 below.

DE-A 199 39 112 describes thermoplastic polyurethanes having a hardness of from Shore 50 A to 75 A. The experimental products according to examples 9, 10 and 11 of DE-A 199 39 112 are based on polyesterdiol PD0 1, like the products according to examples 10, 11 and 12 of the present invention.

TABLE 17 Hardness DE-A 199 39 112 Example 9 73 A Example 10 66 A Example 11 58 A According to the invention Example 10 57 A Example 11 65 A Example 12 71 A

Example 25 Processability by Injection Molding

The products mentioned in table 15 were processed on an injection molding machine, type ES 330/125 from Engel, under optimized conditions to give a round disk having a diameter of 120 mm and a thickness of 2 mm. Optimized conditions mean that, for each individual product, the injection conditions, the temperature profile of the injection unit and the hot runner, and the tool surface temperatures were varied and optimized until a homogeneous, planar round disk having good demoldability and dimensional stability resulted. The cycle times determined after such a process represent a good comparative standard for rating the processability, shorter cycle times being positively rated.

TABLE 18 According to the DEA 199 39 112 invention Examples Examples 11 10 9 10 11 12 Hardness (Shore) 58 A 66 A 73 A 57 A 65 A 71 A Cycle time (sec) 100 90 75 45 40 35

Example 26 Processability by Extrusion (Production of Blown Films)

The products described in table 15 were processed to give blown films on a Brabender laboratory unit comprising melting extruder, film blowing head and take-off apparatus. After appropriate optimization of the extruder temperature profile, of the annular gap width of the film blowing head, of the blow air flow rate and of the take-off speed, satisfactory blown films could be produced and wound in all cases. In case of the products according to DE-A 199 39 112, however, the transparent blown films stuck together to such an extent during winding that the spool could no longer be unwound later on without destruction of the film. Owing to the strong adhesion, it was also impossible to blow up the tubular film.

The novel products on the other hand gave slightly opaque tubular films without any tendency to stick. The spools were always readily unwindable later on and the tubular film itself could be blown up without problems. There were no detectable differences between the individual hardness gradations with respect to tendencies to adhere. 

1. A process for the preparation of thermoplastic polyurethanes, wherein (i) a thermoplastic polyester is reacted with a diol (c) and then (ii) the reaction product of (i) containing (b1) polyesterdiol having a number average molecular weight of from 1000 to 5000 g/mol and a melting point greater than 150° C. and, optionally, (c) diol together with (b2) polyetherdiols and/or polyesterdiols, each having a melting point of less than 150° C. and a number average molecular weight of from 501 to 8000 g/mol and, optionally, further (c) diols having a number average molecular weight of from 62 to 500 g/mol are reacted with (a) isocyanate, in the presence or absence of (d) catalysts and/or (e) assistants.
 2. A process as claimed in claim 1, wherein the molar ratio of the (c) diols having a number average molecular weight of from 62 to 500 g/mol to the component (b2) in the reaction (ii) is less than 0.2.
 3. A process as claimed in claim 1, wherein the thermoplastic polyester has a number average molecular weight of from 15000 to 40000 g/mol.
 4. A process as claimed in claim 1, wherein the thermoplastic polyester used is a polyalkylene terephthalate and/or a poly-L-lactic acid.
 5. A process as claimed in claim 1, wherein the thermoplastic polyester is melted at from 180 to 270° C. and the reaction (i) with the diol (c) is carried out at from 240 to 280° C.
 6. A process as claimed in claim 1, wherein the reaction of the thermoplastic polyester with the diol (c) is carried out in the presence of a catalyst.
 7. A process as claimed in claim 1, wherein butane-1,4-diol and/or ethane-1,2-diol are used as diol (c) in (i) and, optionally, in (ii).
 8. A process as claimed in claim 1, wherein the reactions (i) and (ii) are carried out in a reaction extruder.
 9. A process as claimed in claim 8, wherein the reaction extruder has neutral and/or backward-conveying kneading blocks and backward-conveying elements in the region in which the thermoplastic polyester is melted and screw mixing elements, toothed disks and/or toothed mixing elements in combination with backward-conveying elements in the region in which the thermoplastic polyester is reacted with the diol.
 10. A process as claimed in claim 3, wherein, in the reaction (ii), the ratio of the isocyanate groups to the hydroxyl groups is from 1:1 to 1.2:1.
 11. A process for the preparation of thermoplastic polyurethanes, wherein (i) a thermoplastic polyester is reacted with a diol (c) and then (ii) the reaction product of (i) containing (b1) polyesterdiol having a melting point greater than 150° C. and, optionally, (c) diol together with (b2) polyetherdiols and/or polyesterdiols, each having a melting point of less than 150° C. and a number average molecular weight of from 501 to 8000 g/mol and, optionally, further (c) diols having a number average molecular weight of from 62 to 500 g/mol are reacted with (a) isocyanate, in the presence or absence of (d) catalysts and/or (e) assistants, wherein the molar ratio of the (c) diols having a number average molecular weight of from 62 to 500 g/mol to the component (b2) in the reaction (ii) is less than 0.2. 